Process for pyrolysis of liquid hydrocarbons



April 19, l1938.

J. F. DONNELLY vPROCESS FOR PYROLYSIS` OF LIQUID HYDROCARBONS 4 Sheets-Sheet l Filed March 30, 1934 SSD E WNY H MN Qui@

April 19, 1938-.

' J. F. DONNELLY PRocEss 'FOR PYRoLYsIS oF LIQUID HYDRocARBoNs 4 sheets-sheet 2 Filed March 50, 19554 April 19, 1938.

VFiled March 30, 1934 4 Sheets-Sheet 3 .SOL IDS SU Y FEED Of DECOMPOSH BLE V4 mvp 64555 5 JTEAM, GA3, of A16/1r 01A 44pm? v\ 4 30 727 campe/vise En x y warfam me Apn'119,193s. F.DONNELL -I 2,114,416

PRCESS FOR PYRQgJYSIS OF LIQUID HYDROCARBONS Filed March 30, 1934 4 Sheets-Sheet 4 VII/70A 727 (ONUE'YJER UP FIP/767:@ FROM JOL/B5 PRNI'fl/'YG WV/'f v caa mi: all. WA ff@ COOLER Psanted' Apr. 1s, 193s HYDBOC PATENT-omer Joseph F. Donnelly, Lemont, Ill. .lamination Maren so, 1934, sen-1u No, 71s,1s1

IMy inventionrelates 'to a process for the pyrolysis of hydrocarbons and particularly to the heat treatment of petroleum hydrocarbons of complex character, whereby suchihydrocarbons` 5 are converted into lighter hydrocarbons and' residual products of solid character. More particularly, my invention relates to a process whereby heavy hydrocarbon oils are converted into lighter hydrocarbon oils, together with the formation of coke through the pyrogenic treatment of hydrocarbon oils. l

An object of my invention is to produce commercial products which may be. exemplied by the production of liquid hydrocarbons, such as gasoline, Diesel-engine distillate fuel, furnace oil, gas oil, lubricating oil distillate, etc.. kand heavier re sidual products such as fuel oil, together with solid end products such as coke. 1

Another object'of my invention is the producn tion of coke by progressive building up of separated ,coke masses by progressive pyrogenic decomposition of heavy hydrocarbon oils deposited upon the surfaces of the maintained separated u Another object of my invention is to produce relatively uniform bodies of coke in an automatic and progressive manner. A further object of my invention is to treat coals so as to recoverthe volatile constituents thereof. i

. I have devised a.novel form of apparatus for carrying out my proce and illustrate the preferred form thereof in the drawings, in which Eigure 1 is a processing flow diagram and shows one method of applying the present inventionin lconjunction'with apetroleum refining process.

Figure 2 is a side elevation partly in section of a preferred apparatus for carrying out the invention. y

Figure 3 is anend elevation partly in'section of the apparatus shown in Figure2.

Figure 4 is an end elevation partly in. section of a modified form of the appfratus shown in Figure 3. n

In carryingout my process` with the preferred form of apparatus herein shown, crude oil or its derivatives, such as toppedr crude,gas oil; or oil derived from coal, shale, wood, vegetable or ammal, etc., is supplied by pump I, from any suitable source to'heat exchangers 2 and 3 where it is indirectly heated by the hot vapors passing through said heat exchangers. The preheated charge oil is then .mixed with the eilluent from a highly heated cracking 0r distilling coil l2, as controlled by the adjacent valve l, the mixture being then. l passed into high pressure vapor separator I,

naphtha, etc., either as liquid 130mm- (cl. 19e-4s)- boilingpoints over approximately 650 F,- The fractions having boiling points under 650'? F. re

maining as'vapor are then passed through coil 1, mi

in furnace 8, where they are heated to a temperature sumcient to eilect carbonization rof decomposable oil. being applied to the-agitated carbon bed 9, contained in semi-circular shell 9 of the carbonizr Ill. For illustration the-productsleav 15 ing coil 1, will range from 800 F. to 1200 F., or l higher, depending on the amount of heat to be transmitted thereby. to the carbonizer I0. The vapor or gasesin .coil 1 .may therein be subjected to any desired degree of molecular alteration.

/Semi-circular plate 9' is initially charged with carbonaceoussolid particles. such as. coke, coal. charcoal'or the like, or with .metallic masses of n suitable size andshape, t0 provide a bed of suitf able volume, preferably sumcient toadsorb the 25 decomposable liquid supplied thereto for decomposition. v

The bed is preferably heated suiliciently to effe'ct decomposition and carbonization. as hereinafter described, before supplying decomposable 3o oilthereto.

It is to be understood that the specific temperatures andpressures etc., herein given are for il-i lustrative purposes, and are intended only as examples to promote a better 'understanding of the 35 lteaching of the invention, Aand may be employed within wider or narrower limits than shown without departing' from the fundamentals of the process.

Pressure on the vapor separator may' be con- 40 trolled by regulating valves Il, I2 and I3, or Il, and closing valves I 5 and I6.- If desired, I'may mix` fixed gas such as natural orcracking still gas, or light hydrocarbons, such as crude gasoline,

or vapor, with the. 45 vapors entering heating coil 1, which ymay therein be subjected to any desired degree of molecular alteration, same being supplied from any convenient source by pump, or compressor l1 Athrough valve Il. The highly heated gas and vapor is 50 passed by perforated pipes I9. controlled. by valves Il through-bed 9, to which it imparts heatA` and partial pressure -eil'ect suillcient to effect rapid carbonization of the oil coating the surface of the particles composing the said bed.v Aist The liquid remaining in the vapor separator 5, is delivered by pump to coil 2|, where it is heated under pressure controlled by valve 22, to a temperature suflcient to effect vaporization in vaporizer 23, of substantially all fractions having boiling point lower than that necessary to produce petroleum asphalt, the object being to effect concentration of the highly' complex hydrocarbons inthe liquid residuum. The hot concommingled therewith either at the point 29 or as shown through header 30 controlled by valves 3l. If desired, I may heat the residuum above referred to in a furnace or other means'before entering the carbonizer, in which case the residuum will be heated to the maximum temperature without carbon fouling the heating means.

The vapors leaving the carbonizing element IU,

pass through heat exchanger 3, `thence between the jacket and shell of the'carbonaceous solids preheater 32, where it preheats the carbonaceous solid material which is subsequently treated in carbonizing element lli, or if desired the said vapor may be passed under reduced pressure1 di- 'rectly to condenser 33, by opening valve 34, and

closing valves and 31 and operating vacuum producing means 43', or the vapor leaving preheater 32, may be passed to condenser 33 as above, or to vaporizer 23, by manipulation of valves 34, 35, 31 and 38, in a 'manner well understood to those skilled in the art. `Condensates from exchanger 3 are delivered by pump 39 to vaporizer 23, or may be delivered to the fresh oil line entering exchanger 2, depending on its characteristics, or it may be withdrawn from the system. The vapor leaving vaporizer 23, passes through exchanger 2, then to bubble tower 40, where the desired degree of fractionation is effected. The fractionated vapors are condensed in condenser 4i and the gases separated in'gas separator 42. If desired elements 23, 46, 4|, 42

and 46, may also be operated under reduced pressure by means 43. From the foregoing, it will be seen that the vapor from the carbonizer I0 and from the vaporizer 23, may be fractionated and'condensed separatelyand under different pressures, or may-be commingled, fractionated and condensed together.V Condensates separatd inseparator 43, are preferably delivered by pump 44, to bubble tower 40 for retreatment, or may be withdrawn from the system through valve 44'. The* temperature of the tower 40, -is preferably controlled by trimming with condensate's from separator 42, delivered thereto by pump 45. Products condensing in tower 40, are separated therein into two fractions of different boiling points, the lighter fraction thereof being withdrawn from .the upper-plates to a stripping tower 46, where it is stripped of its most volatile fractions .which are returned as a vapor to the Y. stocksY for reactive heat treatment in the system,

or eachnay be withdrawn from the system through cooler 48, by manipulation of valves it,

49', 50 and 56. Distillate from separator 42, controlled by valve 50, bubble tower 40, stripper 46, or from an extraneous source or mixtures thereof, is delivered by pump 5I, to the inlet of coil 52, in furnace 53, where it is heated for sufflcient time and to sucient temperature to effect either distillation or'cracking in any desired degree and amount within practical operating limits of the balance of the system, and with particular reference tothe process of the invention,

the eiiluent of coil 52, being controlled by valve- 53' and enters separator 5, mixed with preheated fresh charge oil as heretofore explained. While I have shown .the present invention operating in conjunction with a coil type cracking operation it is to be understood, that the invention is not limited to or dependent on conjunctive operation with any particular type of distilling or cracking process, but may be operated successfully with several known cracking processes, or if desired the process of the invention may be operated independently as a separate unit.

Adjustable equal-spaced mixing and separating blades 54, are attached to hollow cooled shaft 55, which rotates counter clockwise; the number of revolutions for a given time being regulated to prevent'the carbonaceous masses from being consolidated into a solid and to remove therefrom carbonaceous particles that have -attained the predetermined size, such particles being too large to pass between the. blades will be carried thereby until an angle is reached where the particles will fall toward the shaft by gravity. The particles will then be intercepted. by grid plate 56, attached to hollowvcooled shaft 51, which will now be operated from shaft 55er independently to elevate the plate 56, to permit the blades 54 to pass, and to discharge the carbon particles accumulated thereon, which particles will descend into the bottom of shell I 0, whereiit will be conveyed vto cooler 60, by screw convey'or 58, having a hollow cooled shaft and which n'iay be operated independently, valve 6| beingv open. Shaft 55, is driven through gear 59, by any suitable power means, not shown. During this operation superheated steam may be passed into the bottom of drum 6|!k through valve 62, to prevent heavy oil vapors from entering and condensing therein. It being understood that drums i0 and 60, and all otherv parts of the apparatus are well insulated where it is desired to prevent heat loss or condensation. During the accumulation of carbon in drum 60, valves 63, 64, 65 and 66 are closed.

When it is desired to empty the drum of its accumulated carbon, conveyor 58 is stopped, additional steam is admitted through valve 62, 'to thoroughly purge the drum of any vapors that may be therein. When this is attained, as may be determined by withdrawing vapors from the top of the drum through a small water cooled coil (not shown), attached thereto for the pur-- pose, and testing the condensates thus obtained for oil. When the drum 60 is sufficiently purged of oil vapors to prevent danger of re, then valve is open to the atmosphere,or maybedisposedof as desired. Valve 63 may now be slightly opened to 4admit a small quantity of cooling water through a spray device. The cooling is continued until the carbon has reached a temperature below its auto ignition point when exposed to the atmosphere. It is then removed 'from the bottom of the cooler and conveyed to storage by any suitable means not shown. It is to be understood that the carbon may becooled` in any suitable ,manner before or after removal. When the drum u admitted through valve 82 and out through valve I4, this operation being continued until all air is expelled from the drum. Any condensed water is withdrawn through drain valve B6, valve 54 is now closed and valve 6| is opened and conveyor 58 is again started. Drum 60 is also equipped with safety pressure valves not shown.

Fresh carbonaceous solid material to be treatv ed is suppliedfrom any suitable source to preheater 32, through supply. means 61, valve 68, being closed. In the preferred method the preheater 32, is charged with small particles of coke,

or coal, or other carbonaceous solid, and vis therein preheated to the maximum temperature obtainable from the vapors employed 'for preheating, this preheating may be done in any suitable manner. Air is prged from the preheater 32, by admitting superheated steam through valve 69, valve 10, being open, valve 1| and valve 12 being closed. Vapor or gas is purgedfrom the preheater 32 by'admitting spperheated steamv through valve valve 1I being open. When the preheater'drum is completelypurged of all air, valves 69, 10 and 12 are closed, valves 6 8 are opened, and screw feed conveyor 13 is operated by any suitable motive means (not shown), to feed carbonaceous material -in a regulated manner to the carbonizing bed 9 as required.` Valve Il is open and any volatile matter contained in the carbonaceous material vaporizable at the temperature prevailing in the preheater will be 'vaporized and removed from the preheater through valve 1I.

fed to thecarbonizing bed 9,' will serve as nuclei for the progressive building up thereof into predetermined sizeparticles by the carbonization on its surface of the complex constituents of the f oil sprayed thereon through spray nozz1es'29.

From the foregoingit will be seen that the concentrated substantially carbon saturated oil to be decomposed; in heated condition is sprayed in nelydividedform, onto the material composing the carbonizirig bed 9," and the highly heated `vapors or gases from an extraneous-source are passed through the bed thus imparting to the decomposable oil coating the surfacesand in the interstices -of the particlescomposin'g the bed suicient heatv and partial pressure effect to rapidly vaporize volatile constituents and eile'ct carbonization of complex fractions contained in or sprayed on the bed 9. It will beobvious that the higherthe temperature of the decomposable` oil before contacting the carbonizing bed, and

the higher the temperature of the vapor, gas, or.

steam passing through the bed, the more accelerated will be the rate of decomposition and carboncarbon thatwill vsubstantially completely vaporize when released through the nozzles 29. By

thisl method of carbonization of decomposable' giluid there results a final carbon `desixlmliacteristics-such a`s a v'high degree of mass density, in contradistinction to porous product having 69, valves 'i0 and 12 being closed,A

Thel finely divided preheated carbonaceous materialV preheat the same directly.-

then introducing the f ,As aj. solvent or diluent; I preferto use a liquid hydrocontinuous carbonizing process .for the production of predetermined size particles, thus eliminating the expense incident to manufacturing briquettes from carbonaceous. material. However, if it is desirable tov produce very fine carboniparticles, such as powder, it may be accomplished by this process. TheA operation will be the same as when making the larger size particles with the apparatus heretofore described, except, the semi-circular carbon-bed plate 9'., will be slotted or perforated in the area beneath the carbon bed and between the particles to fall through said plate. The plate 56, will be permanently elevated during this operation. The shaft 55 andblades 54, will berotated at a speed to produce'an attritional grinding effect of the particles constituting the bed. 9, 'resulting in physical disintegration of generated carbon, the operation rate of carbonization, and of carbon physical disintegration are synchronized so that they'are substantially equal.

When making very fine carbon particles I may replace the carbonaceous material of bed 9, with metal particles of suitable size, preferably spheri- 'cal in shape, to produce a carbonizing surface,

pipes I9 to permit ne being conducted so that the the blades 54 and shaft 55, being 'rotated atv sufcient speed to cause physical disintegration o f the carbon formed on the surface of the metal particles. If desired, the carbonizing apparatus .i0 may be directly heatedby a fur-nace as shown in Fig. 4, in which case the processing operation may be the same as .heretofore described, orit may be conducted without passing hot oil vapors,

gas or steam through the .carbonizing bed 9, in vwhich case Iprefer to employ light oil vapors,

gas, or steam to aid in removing the generated vapors from thecarbonizinggapparatus lll. Such vapor, gas or steam may ent r above the carbonizing bed to sweep away thevapors generated by the bed and released supplied. through nozzles 29.` The vapor, gas or steam above referred to may be supplied by pipes not shown. paralleling oil distributing pipes 28,

said vapor, gas or steam being of sufficient temperature that it will not cause material condensation of generated vapors.- While I have herein described carbonization with the use `0i? vapor, gas or other iiuid, it'is to be understood that while I prefer the use of such, its use is not absolutely essential to effect ycarbonization with the apparatus shown in Fig; 4. Further, while I prefer to operate the process ina substantially continuous manner as heretoforedescribed, ,it is within the scope of the invention to operate the-process as bythe decomposable oil a batch operation, in which case using the carbonizing apparatuses shown, the element 56. would not be in use during carbonization, and the blades 54 anclv shaft 55, would be rotated or oscillated to prevent consolidation of the carbonaceous masses, I may employ a carbonizing element I0, of simple cylindrical shape, the'v balance of the apparatus and the opera-tionin each case be-y ing substantially as heretofore` jdescribed.`

It is to be understood Athat carbonization maybeconducted withoutsubstantial molecular altera- -tion taking placein coil T or 52, the essential condition in such case being that the material heatedr in these' coils lis of sumcient 'volume and attains sufficient temperature therein to accomplish the desired degree of vaporization and superheat necessary to perform the functions intended by 'its use in the process.v

. vIt is to be understood that heat and pressure measuring instruments will be used at all points in the unit where desirable. The unit will also be equipped with sampling devices where needed, also with safety pressure devices. In Figs. 2,v 3 and 4, I have shown a method for cooling the various shafts employed in carbonizer |0, involving the construction of said shafts in hollow lform through which a stream of cooling uid is,

circulated. Lines containing valves l5. I6 and 65, are used only when starting or stopping operations, at which time these valves are manipulated to permit flow through the respective lines as indicated by" arrows. It is to be understood that the process of this invention may be carried out as herein described when using heated fluids such as iiue gases, hydrocarbon gases, including Water gas, hydrocarbon vapors, inert gases, steam, etc., or mixtures thereof. The invention is not limited in its application to the specific apparatuses shown, which are only of preferred form capable of carrying out the invention, the size, shape,

carbons and producing cracked vapors while progressively depositing carbon on said particles,

.respectively releasing and withdrawing from said zonelsaid vapors and accreted carbon particles exceeding said restricted size, dephlegmating and condensing out of the released vapors preferred fractions, and returning to the process less preferred fractions for pyrolysis as aforesaid.

2. 'A process for the pyrolysis of hydrocarbons which comprises subjectinga limited quantity of carbonaoeous mattersuch 'as coalto a coking temperature in a closed zone under disintegrative mechanical classification and producing coke 'particles of restricted size, discharging said hydrocarbons on said particles maintained in said zone at said coking temperature and producing cracked vapors while progressively depositing carbon on said particles, respectively releasing and withdrawing from said zone said vapors and accreted carbon particles exceeding said restricted size, dephlegmating and condensing out of the released vapors preferred fractions, and returning to the yprocess less preferred fractions for pyrolysis as aforesaid.

3. A process for the pyrolysis of relatively heavy hydrocarbons which comprises subjecting a limit- :ed quantity of coal to a coking temperature in a closed zone under disintegrative mechanical classification and producing coke particles of -limited maximum and less size, discharging said hydrocarbons on said particles maintained in said zone at said coking temperature and producing cracked vapors lwhile progressively depositing carbon on said particles, respectively releasing and withdrawing from said zone saidr vapors and accreted carbon particles exceeding said maxi- -mum size while effecting inorescence of carbon particles of less size, dephlegmating andvcondensing out of the released vapors preferred fractions, and returning to the process less preferredf fractions for pyrolysis as aforesaid.

4. A process for the pyrolysis of 'relatively heavy hydrocarbons which comprises discharging such hydrocarbons on ccarbon particles of limited maximum and less size disposed in a coking zone wherein said particles are mechanically agitated and classified at the coking temperature of said hydrocarbons, dissociating the latter into vapors and carbon, progressively depositing said carbon on said particles, respectively releasing and withdrawing from said zone said vapors and accreted carbon' particles exceeding said maximum size while effecting inorescence of carbon particles of less size, dephlegmating and condensing out of the released vapors preferred fractions, and rcturning to the process less preferred fractie for pyrolysis` as aforesaid.

5. A process for the pyrolysis of petroleum hydrocarbons which comprises discharging such hydrocarbons on coke particles of limited maxim'um and/less size disposed in a coking zone wherein said particles are mechanically agitated and classified at the coking temperature of said hydrocarbons, dissociating the latter into gasoline-` containing vapors and carbon, progressively depositing said carbon on said particles, respectively releasing and withdrawing from said zone said vapors and accreted carbon particles exceeding said maximum size while effecting inorescence of coke and carbon particles of less size. dephlegmating and condensing out of the released vapors gasoline, and returning to the process nongasoline fractions for pyrolysis as aforesaid,

6. A process for the pyrolysis of petroleum hydrocarbons which comprises discharging such hydrocarbons on coke particles of limited maximum and less'size disposedina coking zone wherein said particles are maintained under mechanical agitation and classification at the `coking temperature of said hydrocarbons through indirectly applied heat, dissociating said hydrocarbons into drocarbons which comprises discharging such hydrocarbons on a limited quantity of coke particles of ycontrolled maximum and less size disposed in a coking zone wherein said particles are maintained under mechanical agitation and classification at the coking temperature of lsaid hydrocarbons through heat exteriorly applied to said zone, dissociating said hydrocarbons into 'gasoline-containing vapors and carbon, progressively depositing said carbon on said particles, respectively releasing and withdrawing from said zone-said vapors and .carbon accreted particles exceeding s aid maximum size while effecting in.- crescence of coke and carbon particles ofrless size, dephlegmating and condensing out ofthe released vapors gasoline, and returning to the v. process non-gasoline fractions for pyrolysis 'as aforesaid.

8. A process for the pyrolysis of relatively discharging such' hydrocarbons on a-fliinited quantity o`f coke particles of controlled maximum andfless size disposed in a colnng zone wherein said particles are maintained under mechanical agitation and classification at the coking tem-` perature of saidhydrocarbons through contact with heat'ed hydrocarbon vapor, dissociating said hydrocarbons into gasoline-containing vapors and carbon, progressively depositing said carbon on said particles, respectively releasing and withdrawing from said zone hydrocarbon vapors and accreted 'carbon particles exceeding said maximum size while effecting increscence of coke and carbon particles of less size, dephlegmating and condensing out of the released hydrocarbon vapors gasoline, -and returning to the process nongasoline fractions for pyrolysis as aforesaid.

` 9. A process for the pyrolysis of relatively heavy petroleum hydrocarbons whichcomprises discharging such hydrocarbons on a limited quantityw of coke particles of controlled maximum and less size disposed in a coking zone wherein said particles are maintained vunder mer chanical agitation and classication at the cokingtemperature of said hydrocarbons through contact with a stream of heated hydrocarbon vapor substantially undecomposed at said coking temperature, dissociating said hydrocarbons into gasoline-containing vapors and carbon, progressively depositing-said carbon on said particles,

' respectively releasing and withdrawing from said zone hydrocarbon vapors and accreted carbonparticles exceeding said maximum size while effecting increscence of coke and carbon particles of less size, dephlegmating and condensing out of the released hydrocarbon vapors gasoline.

and returning to the process non-gasoline fractions for pyrolysis as aforesaid.

10. A process for the pyrolysis of relatively.

heavy petroleum hydrocarbons which comprises discharging such hydrocarbons on a limited" quantity of coke particles of controlled maxi-- mum and less size disposed in a coking zone wherein said particles are maintained under me-` chanical agitationand classification at thecoking temperature of saidhydrocarbons through heat exteriorly applied to said zone and contact `witli'a stream of heated hydrocarbon vapor sub-fl stantially undecomposed at said coking'temperature, dissociating said hydrocarbons into gasoline-containing vapors and carbon progressively depositing said carbonon said particles, respectively releasing-and withdrawing from said zonev hydrocarbon vapors and accreted carbon particles exceeding said maxlmum'size while effecting increscence of coke and carbonv particles of less size, dephlegmating and condensing out of the released hydrocarbonvapors' preferred gasoline fractions, and returning to the process uncondensed hydrocarbon vaporand relatively heavy residual `fractigms resultingI from vauch dephlegmation-,for pyrolysis as aforesaid.

11, A.v process for the pyrolysis of .heavy petroleum hydrocarbons which comprises progressively deposi respectively releasing and withdrawing from saidy carbons on coke .particles of limited and less size disposed in a coking zone wherein 'said particles are maintained under mechanical bon particles exceeding said maximum sizewhilel Y effecting increscence of coke and carbon particles of less size, dephlegmating `and condensing out oftheA expelled hydrocarbon vapors preferred gasoline fractions, and returning to the process uncondensed hydrocarbon vapor and rel-l atively,heavy residual fractions resulting from vsuch dephlegmation for pyrolysis as aforesaid.

12. A cyclicprocess for the pyrolysis of relatively heavy petroleum hydrocarbons into gasoline-containing light hydrocarbons and carbon which comprises converting said relatively heavy hydrocarbons into distillate and residual fracparticles` o1' hunted maximum and less size disposed in a coking zone wherein said particles are maintained under mechanical agitation and classication at the coking temperature of said residual fractions by contact with 'a stream of hydrocarbonl vapor derived from' said distillate fractions and heated to the. oo king temperature of said residual fractions, dissociating said re-l sidu'al fractions into gasoline-containing vapors and carbon, progressively depositing said carbon onsaid particles and expelling from said zone said vapors by said stream of hydrocarbon vai por., withdrawing'frcm saidl :one carbon accreted particles exceeding said maximum size while `ef` fecting increscence of coke and carbon particles of less size, dephiegmatingyand condensing out' of the expelled hydrocarbon vapors gasoline, and

returning to the process non-gasoline fractions from such vdephlegmation for further conversion `and rproduction of residualfractions for pyrolysis as aforesaid. l

13.y A process for the pyrolysis of hydrocarbons which comprises subjecting a limited quan- -tity of solid carbonaceous matter substantially reducible to carbon by pyrolysis to a carbonizing temperaturev in a closed zone under disintegrative mechanical .classication and producing car-y bon particles of restricted size, discharging said hydrocarbons on said .particles maintained in said zone at the coking temperature of said hydrocarbons and producing cracked Avapors while g carbon on said particles,

zone said vaporsv and accreted carbon particles exceeding said restricted size, and condensing the released vapors. -v

. JQBEPB F. QONNRLLY.

u tions, discharging said residual fractions on coke 

